US5956971A - Process for liquefying a natural gas stream containing at least one freezable component - Google Patents

Process for liquefying a natural gas stream containing at least one freezable component Download PDF

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Publication number
US5956971A
US5956971A US09/105,845 US10584598A US5956971A US 5956971 A US5956971 A US 5956971A US 10584598 A US10584598 A US 10584598A US 5956971 A US5956971 A US 5956971A
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stream
liquid
methane
separation system
pressure
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US09/105,845
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Eric T. Cole
Eugene R. Thomas
Ronald R. Bowen
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ExxonMobil Upstream Research Co
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Exxon Production Research Co
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
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    • F25J1/0244—Operation; Control and regulation; Instrumentation
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    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
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    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/30—Dynamic liquid or hydraulic expansion with extraction of work, e.g. single phase or two-phase turbine
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/90—Processes or apparatus involving steps for recycling of process streams the recycled stream being boil-off gas from storage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/10—Control for or during start-up and cooling down of the installation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/40—Control of freezing of components
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S62/00—Refrigeration
    • Y10S62/928—Recovery of carbon dioxide
    • Y10S62/929—From natural gas

Definitions

  • This invention relates to a natural gas liquefaction process, and more particularly relates to a process to produce pressurized liquid natural gas (PLNG) from a natural gas stream containing at least one freezable component.
  • PLNG pressurized liquid natural gas
  • LNG liquefied natural gas
  • a first portion of the liquefied stream is withdrawn from the process as a pressurized liquefied product stream (PLNG).
  • a second portion of the liquefied stream is returned to the separation system to provide refrigeration duty to the separation system.
  • PLNG pressurized liquefied product stream
  • a vapor stream is withdrawn from an upper region of the separation system and is compressed to a higher pressure and cooled.
  • the cooled, compressed stream is then expanded by an expansion means to produce a predominantly liquid stream.
  • a first portion of the liquid stream is fed as a reflux stream to the separation system, thereby providing open-loop refrigeration to the separation system, and a second portion of the liquid stream is withdrawn as a product stream having a temperature above about -112° C. (-170° F.) and a pressure sufficient for the liquid product to be at or below its bubble point.
  • a still further object of the invention is to provide a more efficient liquefaction process by keeping the process temperature for the entire process above about -112° C., thereby enabling the process equipment to be made of less expensive materials than would be required in a conventional LNG process that have at least part of the process operating at temperatures down to about -160° C.
  • the very low temperature refrigeration of conventional LNG process is very expensive compared to the relatively mild refrigeration needed in the production of PLNG in accordance with the practice of this invention.
  • FIG. 2 is a schematic representation of a cryogenic, CFZ process generally illustrating an open-loop refrigeration cycle for producing pressurized liquefied natural gas in accordance with the process of this invention.
  • bubble point is the temperature and pressure at which a liquid begins to convert to gas. For example, if a certain volume of PLNG is held at constant pressure, but its temperature is increased, the temperature at which bubbles of gas begin to form in the PLNG is the bubble point. Similarly, if a certain volume of PLNG is held at constant temperature but the pressure is reduced, the pressure at which gas begins to form defines the bubble point. At the bubble point, PLNG is saturated liquid. It is preferred that the PLNG is not just condensed to its bubble point, but further cooled to subcool the liquid. Subcooling the PLNG reduces the amount of boil-off vapors during its storage, transportation and handling.
  • the energy needed for liquefying natural gas containing significant concentrations of a freezable component such as CO 2 is greatly reduced over energy requirements of a conventional process for producing LNG from such natural gas.
  • the reduction in necessary refrigeration energy required for the process of the present invention results in a large reduction in capital costs, proportionately lower operating expenses, and increased efficiency and reliability, thus greatly enhancing the economics of producing liquefied natural gas.
  • the raw natural gas feed stock suitable for the process of this invention may comprise natural gas obtained from a crude oil well (associated gas) or from a gas well (non-associated gas).
  • the raw natural gas often contains water, carbon dioxide, hydrogen sulfide, nitrogen, butane, hydrocarbons of six or more carbon atoms, dirt, iron sulfide, wax, and crude oil.
  • the solubilities of these contaminants vary with temperature, pressure, and composition.
  • CO 2 , water, and other contaminants can form solids, which can plug flow passages in cryogenic heat exchangers.
  • One advantage of the present invention is that the warmer operating temperatures enables the natural gas to have higher concentration levels of freezable components than would be possible in a conventional LNG process.
  • the CO 2 in a conventional LNG plant that produces LNG at -160° C., the CO 2 must be below about 50 ppm to avoid freezing problems.
  • the natural gas can contain CO 2 at levels as high as about 1.4 mole % CO 2 at temperatures of -112° C. and about 4.2% at -95° C. without causing freezing problems in the liquefaction process of this invention.
  • a natural gas feed stream 10 enters the system at a pressure above about 3,100 kPa (450 psia) and more preferably above about 4,800 kPa (700 psia) and temperatures preferably between about 0° C. and 40° C.; however, different pressures and temperatures can be used, if desired, and the system can be modified accordingly.
  • the gas stream 10 is below about 1,380 kPa (200 psia), it can be pressurized by a suitable compression means (not shown), which may comprise one or more compressors.
  • a suitable compression means not shown
  • the natural gas stream 10 has been suitably treated to remove water using conventional and well known processes (not shown in FIG. 1) to produce a "dry" natural gas stream.
  • Feed stream 10 is passed through cooler 30.
  • the cooler 30 may comprise one or more conventional heat exchangers that cool the natural gas stream to cryogenic temperatures, preferably down to about -50° C. to -70° C. and more preferably to temperatures just above the solidification temperature of CO 2 .
  • the cooler 30 may comprise one or more heat exchange systems cooled by conventional refrigeration systems, one or more expansion means such as Joule-Thomson valves or turboexpanders, one or more heat exchangers which use liquid from the lower section of the fractionation column 31 as coolant, one or more heat exchangers that use the bottoms product stream of column 31 as coolant, or any other suitable source of cooling.
  • the preferred cooling system will depend on the availability of refrigeration cooling, space limitation, if any, and environmental and safety considerations. Those skilled in the art can select a suitable cooling system taking into account the operating circumstance of the liquefaction process.
  • the cooled stream 11 exiting the feed cooler 30 is conveyed into a fractionation column 31 having a controlled freeze zone ("CFZ"), which is a special section to handle solidification and melting of CO 2 .
  • the CFZ section which handles solidification and melting of CO 2 , does not contain packing or trays like conventional distillation columns, instead it contains one or more spray nozzles and a melting tray. Solid CO 2 forms in the vapor space in the distillation column and falls into the liquid on the melting tray. Substantially all of the solids that form are confined to the CFZ section.
  • the distillation column 31 has a conventional distillation section below the CFZ section and preferably another distillation section above the CFZ section.
  • a CO 2 -rich stream 12 exits the bottom of column 31.
  • the liquid bottom product is heated in a reboiler 35 and a portion is returned to the lower section of column 31 as reboiled vapor.
  • the remaining portion (stream 13) leaves the process as CO 2 -rich product.
  • a methane-rich stream 14 exits the top of column 31 and passes through a heat exchanger 32 which is cooled by stream 17 that is connected to a conventional closed-loop refrigeration system 33.
  • a single, multi-component, or cascade refrigeration system may be used.
  • a cascade refrigeration system would comprise at least two closed-loop refrigeration cycles.
  • the closed-loop refrigeration system may use as refrigerants methane, ethane, propane, butane, pentane, carbon dioxide, hydrogen sulfide, and nitrogen.
  • propane Preferably, the closed-loop refrigeration system uses propane as the predominant refrigerant.
  • FIG. 1 shows only one heat exchanger 32, in the practice of this invention multiple heat exchangers may be used to cool the vapor stream 14 in multiple stages.
  • Heat exchanger 32 preferably condenses substantially all of vapor stream 14 to a liquid.
  • Stream 19 exiting the heat exchanger has a temperature above about -112° C. and a pressure sufficient for the liquid product to be at or below its bubble point.
  • a first portion of the liquid stream 19 is passed as stream 20 to a suitable storage means 34 such as a stationary storage tank or a carrier such as a PLNG ship, truck, or railcar for containing the PLNG at a temperature above about -112° C. and a pressure sufficient for the liquid product to be at or below its bubble point.
  • a second portion of the liquid stream 19 is returned as stream 21 to the separation column 31 to provide refrigeration to the separation column 31.
  • the relative proportions of streams 20 and 21 will depend on the composition of the feed gas 10, operating conditions of the separation column 31, and desired product specifications.
  • a minor portion of the vapor stream 14 may optionally be removed from the process as fuel (stream 15) to supply a portion of the power needed to drive compressors and pumps in the liquefaction process.
  • This fuel may optionally be used as a refrigeration source to assist in cooling the feed stream 10.
  • FIG. 2 illustrates in schematic form another embodiment of this invention in which open-loop refrigeration is used to provide refrigeration to the separation column 51 and to produce PLNG.
  • a multi-component gas stream 50 containing methane and carbon dioxide that has been dehydrated and cooled by any suitable source of cooling (not shown in FIG. 2) is fed into a CFZ column 51 which has essentially the same design as separation column 31 of FIG. 1.
  • This embodiment effectively manages the potential for the formation of solids in the liquefaction process by feeding stream 64 directly into CFZ column 51.
  • the temperature of the gas fed into CFZ column 51 is preferably above the CO 2 solidification temperature.
  • a methane-enriched vapor stream 52 exits the overhead of CFZ column 51 and a carbon dioxide-enriched stream 53 exits the bottom of CFZ column 51.
  • the liquid bottom product is heated in a reboiler 65 and a portion is returned to the lower section of the CFZ column 51 as reboiled vapor.
  • the remaining portion (stream 54) leaves the process as CO 2 -rich liquid product.
  • a first portion of the overhead stream 52 is refluxed back to the CFZ column 51 as stream 64 to provide open-loop refrigeration to the CFZ column 51.
  • a second portion of the overhead stream 52 is withdrawn (stream 63) as a PLNG product stream at a pressure that is at or near the operating pressure of the CFZ column 51 and at atemperature above about -112° C. (-170° F.).
  • a third portion of the overhead stream 52 may optionally be withdrawn (stream 59) for use as sales gas or further processed.
  • distillation column 190 which has a CFZ section similar to separation column 31 of FIG. 1, separates the feed into a methane-enriched vapor overhead product and a carbon dioxide-enriched liquid bottoms product.
  • distillation column 190 has at least two, and preferably three, distinct sections: a distillation section 193, a controlled freeze zone (CFZ) 192 above the distillation section 193, and optionally an upper distillation section 191.
  • the incoming feed gas is divided into two streams: stream 102 and stream 103.
  • Stream 102 is cooled in one or more heat exchangers.
  • three heat exchangers 130, 131, 132 are used to cool stream 102 and to serve as reboilers to provide heat to the distillation section 193 of column 190.
  • Stream 103 is cooled by one or more heat exchangers that are in heat exchange with one of the bottom product streams of column 190.
  • FIG. 3 shows two heat exchangers 133 and 141 which warm bottoms products leaving the column 190.
  • feed stream 101 may be cooled by a process stream exiting the top of column 190.
  • the feed stream 101 may be cooled at least partially by conventional refrigeration systems, such as closed-loop single component or multi-component refrigeration systems.
  • Streams 102 and 103 are recombined and the combined stream is passed through an appropriate expansion means, such as Joule-Thomson valve 150, to approximately the operating pressure of the separation column 190.
  • an appropriate expansion means such as Joule-Thomson valve 150
  • a turboexpander can be used in place of the Joule-Thomson valve 150.
  • the flash expansion through valve 150 produces a cold-expanded stream 105 which is directed to the upper part of the distillation section 193 at a point where the temperature is preferably high enough to avoid freezing of CO 2 .
  • a portion of stream 107 after passing through compressor 160 may optionally be withdrawn (stream 128) for use as fuel for the gas processing plant.
  • Another portion of stream 107 after passing through after-cooler 139 is withdrawn (stream 110) as sales gas.
  • the remaining part of stream 107 is passed as stream 108 to heat exchangers 140, 136 and 137.
  • Stream 108 is cooled in heat exchangers 136 and 137 with cold fluids from stream 124 exiting the bottom of column 190.
  • Stream 108 is then cooled further in heat exchanger 145 by heat exchange with overhead vapor stream 106, resulting in warming of stream 106.
  • Stream 108 is then pressure expanded by an appropriate expansion device, such as expander 158 to approximately the operating pressure of column 190.
  • Stream 108 then splits, one portion is passed as PLNG product (stream 126) at a temperature above about -112° C. and a pressure above about 1,380 kPa (200 psia) for storage or transportation.
  • the other portion (stream 109) enters separation column 190.
  • the discharge pressure of compressor 161 is regulated to produce a pressure that is high enough so that the pressure drop across the expander 158 provides sufficient cooling to ensure that streams 109 and 126 are predominantly liquid enriched in methane.
  • additional compression can be installed after compressor 160 and before heat exchanger 136.
  • stream 109 is preferably fed through stream 109A and sprayed directly into the CFZ section 192 through spray nozzle 194. After process start up, stream 109 may be fed (stream 109B) to the upper section 191 of the separation column 190.
  • a CO 2 -enriched liquid product stream 115 exits the bottom of column 190.
  • Stream 115 is divided into two portions, stream 116 and stream 117.
  • Stream 116 passes through an appropriate expansion device, such as Joule-Thomson valve 153, to a lower pressure.
  • Stream 124 that exits valve 153 is then warmed in heat exchanger 136 and stream 124 passes through another Joule-Thomson valve 154 and still another heat exchanger 137.
  • the resulting stream 125 is then merged with vapor stream 120 from separator 181.
  • Stream 117 is expanded by an appropriate expansion device such as expansion valve 151 and passed through heat exchanger 133 thereby cooling feed stream 103.
  • Stream 117 is then directed to separator 180, a conventional gas-liquid separation device.
  • Vapor from separator 180 (stream 118) passes through one or more compressors and high pressure pumps to boost the pressure.
  • FIG. 3 shows a series of two compressors 164 and 165 and pump 166 with conventional coolers 143 and 144.
  • Product stream 122 leaving pump 166 in the series has a pressure and temperature suitable for injection into a subterranean formation.
  • Liquid products exiting separator 180 through stream 119 are passed through an expansion device such as expansion valve 152 and then passed through heat exchanger 141 which is in heat exchange relationship with feed stream 103, thereby further cooling feed stream 103.
  • Stream 119 is then directed to separator 181, a conventional gas-liquid separator device. Vapors from separator 181 are passed (stream 120) to a compressor 163 followed by a conventional after-cooler 142.
  • Stream 120 is then merged with stream 118. Any condensate available in stream 121 may be recovered by conventional flash or stabilization processes, and then may be sold, incinerated, or used for fuel.
  • the separation systems illustrated in FIGS. 1-3 have only one distillation column (column 31 of FIG. 1, column 51 of FIG. 2, and column 190 of FIG. 3), the separation systems of this invention can comprise two or more distillation columns.
  • the first column contains two sections, a distillation section and a controlled freeze zone above the distillation section, and the second column contains one distillation section, which performs the same function as section 191 in FIG. 3.
  • a multi-component feed stream is fed to the first distillation column.
  • the liquid bottoms of the second column is fed to the freezing zone of the first column.
  • the vapor overhead of the first column is fed to the lower region of the second column.
  • the second column has the same open-loop refrigeration cycle as that shown in FIG. 3 for column 190.
  • a vapor stream from the second distillation column is withdrawn, cooled, and a portion thereof refluxed to the upper region of the second separation column.
  • Table 3 shows a comparison of the refrigerant compression requirements for the conventional LNG process and the PLNG process described in simulation example of the foregoing paragraph. As shown in Table 3, the total required refrigerant compression power was 67% higher to produce conventional LNG than to produce PLNG in accordance with the practice of this invention.

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  • General Chemical & Material Sciences (AREA)
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